CN103221141B - Method for processing a product in a centrifugal field and centrifugal machine using the method - Google Patents

Abstract

Method for processing, in particular for clarifying, a liquid using at least one continuously operating centrifuge, in particular a separator with a disc stack (8), wherein a volumetric flow of the liquid is fed into the centrifuge, particles (16, 17) are separated from the liquid and, if appropriate, the liquid is separated into a plurality of liquid phases, and the liquid or the liquid phases and the separated particles (16, 17) are discharged separately from the centrifuge, and wherein the volumetric flow of the liquid is fed in a timed manner continuously or batchwise.

Description

For supplying the method for product and the centrifuge for the method in centrifuges beat-type

Technical field

The present invention relates to a kind of method and a kind of centrifuge, particularly seperator of the product for the treatment of flowing.

Background technology

In the seperator with dish assembly, under static/stable condition, realize particle from liquid or from the intermediate space entering dish, be i.e. be separated in the volume flow in so-called dish gap.The present invention optimizes this working method.

Summary of the invention

Therefore the object of this invention is to provide a kind of method for the treatment of liquid of improvement, and provide a kind of centrifuge, described centrifugal function realizes Working liquids efficiently.

According to the present invention, described object is realized by a kind of method of the product for the treatment of flowing, the method utilizes at least one to process by the centrifuge of continuous operation work, described centrifuge has revolvable bowl, setting dish assembly in described bowl, described method has following steps:

A) in bowl, the described product that can flow is supplied,

B) from the product that can flow, be separated solid phase and/or the separation of products that can flow become two or more liquid phase,

C) by one or more discharge line for liquid phase, one or more liquid phase is derived from bowl, and, when in step b) in when also isolating solid phase, solid phase is derived from bowl,

It is characterized in that,

D) with the product that the volume flow supply of continuously or discontinuously beat-type need process, thus the small product size stream beat-type supplied supply, and need not close at this moment for liquid phase discharge line or additionally throttling is carried out to it.

Described object is also realized according to the centrifuge of method of the present invention for performing by a kind of, it has revolvable bowl, particularly there is the separator drum of vertical-rotation-axis, setting dish assembly in described bowl, described separator drum also has at least one for supplying the input port of the product that need process and at least one is for deriving the outlet of at least one liquid phase and at least one is for deriving at least one other phase, the particularly outlet of liquid phase or solid phase, it is characterized in that, there is the device for making the raw continuous or discrete beat of small product size miscarriage inputted in bowl.

According to the present invention, described for utilize at least one preferably with run continuously work centrifuge, particularly have dish assembly seperator processing, particularly the method for supernatant liquid at least comprise the following steps:

A) by flowable product input bowl,

B) make solid phase separate out from liquid and/or described fluid separation applications become multiple liquid phase and/or a solid phase, and

C) described liquid phase and/or solid phase are derived from bowl,

D) wherein, the supply of the product that need process is realized with the volume flow of continuously or discontinuously beat-type.

In bowl, the product that need process is supplied by beat-type, be formed into the inlet flow of beat-type in the intermediate space between dish gap or dish in centrifuges, thus in corresponding dish gap, form the volume flow of fluctuation or the volume flow reduced in time from a maximum and/or volume flow stop completely." beat-type " this refers to, inlet flow " always repeatedly or many times " repeatedly changes, and or repeat with the beat frequency that the unit interval is constant, or repeat with inconstant beat frequency, but unit interval T1 (such as a minute or a second) is repeatedly.

At low discharge or without in the time period of flow, the particle being conducive to depositing is slipped to rotary drum inner chamber from panel surface.

Preferably on the time period T1 determining duration, supply small product size V1, wherein need the supply of the product processed to carry out like this by the operation of beat-type, the small product size V1 that unit interval T1 is imported in rotary drum does not change relative to the supply of the operation by non-beat-type or keeps constant.This is particularly advantageous, because processing speed does not reduce relative to the operation of non-beat-type generally, however still make use of the advantage that beat-type runs.

Here also especially desirably, the supply beat-type ground of the product that need process carries out like this, make to realize inlet flow (amount) around the increase of a mean value and reduction according to the time, particularly realize like this, make not to be completely interrupted by becoming a mandarin of running of beat.

Known by WO 2005/065835A1, in order to avoid the blocked path of separator when milk being separated into cream (Ram) and defatted milk, determine the fat content of the product phase flowed out, and when more than an extreme value, by changing operational factor in short time, as input power, separated region is moved.But when there is blocking, namely under the exception exceeding extreme value, input power only can disposablely improve here in short time.

Also known by DE 566 199 PA, have in the centrifugal separator of closed housing a kind of, when the discharge line of the supply of material sealing liquid at the same time under stress, impact type ground carries out.This is also for removing blocking.But different from situation in the present invention, supply seasonable discharge line to be closed in impact type.Unlike this, according to the present invention, the diameter for the discharge line of liquid phase remains unchanged, and in other words, supplies the small product size stream beat-type supplied, and need not close at this moment for liquid phase discharge line or additionally throttling is carried out to it.This is due to the stalling characteristic according to the change that present invention utilizes in dish gap, does not need that product is discharged and has beat.

Accompanying drawing explanation

Below with reference to the accompanying drawings according to an embodiment, the present invention is described in detail.Wherein

Fig. 1 schematically shows the phantom of separator drum;

Fig. 2 illustrates the schematic diagram in dish gap; And

Fig. 3 a, b illustrate the figure of separation degree in the volume flow of beat-type and non-beat-type.

Detailed description of the invention

Fig. 1 illustrates bowl, is separator drum 1 here, and described separator drum has vertically-oriented rotation Z.

Revolvable separator drum 1 is arranged in drive shaft 2, and described drive shaft is such as driven directly or is driven by driving-belt and supports revolvably in unshowned mode here.Drive shaft 2 is configured to taper here in circumferential area in the above.Separator drum 1 does not surround with drum rotating, static case 3 by one.This favourable diconical separator drum 1 has the entrance of the input pipe 4 with the product P for processing, described input pipe connects distributor 5, described distributor is provided with at least one or more outlet 6, by the product of described outlet input or centrifugal material by the inside importing dish assembly 8 of separator drum 1.Here coil assembly 8 upwards to be closed by precipitation dish 9 alternatively.Also it is contemplated that the supply line of the distributor 6 using the rising passway 7 entering dish assembly alternatively.Preferably separator disk assembly is set in bowl 1.

Operation is continuous print, in other words, during process centrifugal material, processes centrifugal material constantly and it is derived from centrifuge constantly.

Different from the machine closed in such as DE 566 199 PS, solid is also derived during clarifying from rotary drum, namely by the opening of piston slide valve or derived by nozzle, and need not interrupt for this reason and open the housing of rotary drum.

In centrifugal district, here to the separation of combining of flowable product and/or the clarification of input, form liquid phase L1 and a L2 and solid phase S of two Different Weight here.

According to Fig. 1, after being separated in dish assembly 8, solid phase S is transported in solid output cavity 10 and from being derived by solids outlet 11 discontinuously here, described solids outlet can open and close by means of piston slide valve 12.But the operation of centrifuge, still runs with continuous print the actual treatment of centrifugal material exactly and carries out, because always can derive solid, and need not interrupt rotating for this reason.

Lighter liquid phase L1 is in the radius r of inside _iplace utilizes (unshowned) first skimming device to derive from rotary drum here.Heavier liquid phase L2 flows around the excircle of separator disk 9 and passes through the second skimming device (not shown equally) here on the contrary to derive from separator drum 1.

Schematically show the dish gap between the adjacent dish of dish two of assembly 8 or separator disk 14 and 15 or intermediate space 13 in fig. 2.Inlet flow is the part of volume flow in the inflow dish gap imported, such as radial direction in flakes between, spaced for each rim axial direction turning up the soil keeps and if desired dish gap is divided into multiple sections by described radial direction in flakes.

Inlet flow has two kinds of particles in fig. 2, and wherein the first particle 16 is located at the outer radius r of dish 14 and 15 _aplace, described dish is spaced from each other with gap width h.Second particle 17 to be located immediately between dish 14 and 15 and to have radius r at moment t relative to rotation Z, and this radius is less than the outer radius r of dish 14 or 15 _aand be greater than the inside radius r of dish _i.

Inlet flow is from the outer radius r of dish 14 or 15 _aradius r inwardly _idirection directed, solid portion, as particle 16 and 17 deposits on separator disk.Solid particle from here due to dish inclined angle alpha be slipped to solid output cavity 10.

Separation process occurs in dish gap according to prior art under continuous print inlet flow.This carries out under the condition of stable state/static state substantially.But advantageously show, non-stable inlet flow can cause better separating property.

This is as explained below:

When insignificant little acceleration effect, first little particle follows floating in inlet flow.Here inlet flow or described particle speed v can as on the time t inner radial direction determined the function of distance r (t) of process determined by following formula by the outer circumferential area A in the inlet flow Qt in each dish gap and dish gap:

${\mathrm{\υ}}_{p,r}=\frac{\∂r}{\∂t}=\frac{Q_T}{A}$

Outer circumferential area is particle to the function of the radius r of rotation Z, the dish gap width h in gap and the inclined angle alpha of dish:

$A=2\mathrm{\πr}\frac{h}{\cos \mathrm{\α}}$

When considering outer circumferential area A, the speed therefore for particle and inlet flow can obtain a differential equation of first order under radius r:

$\stackrel{\·}{r}=\frac{Q_T}{2\mathrm{\πrh}}\cos \mathrm{\α}$

By at boundary condition r (t=0)=r _asolve when coiling the flow direction in gap down and at consideration inlet flow, the grain spacing for the radial direction to rotation Z obtains following equation about time t:

$r\left(t\right)=\sqrt{r_a^2-\frac{Q_{T}t\cos \mathrm{\α}}{\mathrm{\πrh}}}$

At r (t)=r _itime the particle maximum time T that stops in gap _endas shown in the formula drawing:

$T_{\mathrm{end}}=\frac{(r_a^2-r_i^2)\mathrm{\πh}}{Q_T\cos \mathrm{\α}}$

The decrease speed of particle in centrifugal district to its to radial spacing of rotation relevant also thus with time correlation, wherein be the density contrast of solid and liquid, d is particle diameter, and ω is angular speed, and η is the dynamic viscosity of fluid.

The sedimentation distance h (T) that particle passes through within the time determined vertical be decrease speed function and as shown in the formula calculating:

$h_p\left(T\right)=\frac{1}{T}\underset{0}{\overset{T}{\∫}}{\mathrm{\υ}}_{\sin k}\left(t\right)\∂t*T$

Bring time variable T into by anomalous integral t and obtain following formula:

Here when particle is when the upper dish in time t arrival dish gap, think that particle is sedimentation.Therefore, when meeting following formula, particle is sedimentation:

h _p，Start+h _p(t)≥h

Wherein t=T _end.

Therefore have

Depend on that therefore the separative efficiency φ (d) of the diameter of particle can be represented by equation below:

For the inlet flow Q of non-static with different functions _tt () can easily utilize Time-marching Method (Zeitschrittverfahren) to solve separative efficiency φ (d) by the mode of numerical value.

Fig. 3 a illustrate from time correlation inlet flow is carried out to the different modification of the control on volume.Such as have input is 1m for each dish here ³/ h.

The known case of continuous print inlet flow illustrates as solid line.

Dotted line represents inlet flow interruption completely in time.Such as supply the amount of four times here in short time, wherein with four intermittent interruption.Inlet flow so generally is also each dish 1m ³/ h.

Dotted line illustrates that inlet flow is around the increase of the sinusoidal of a mean value and time correlation and reduction, but inlet flow does not interrupt completely here.Here inlet flow is also each dish 1m generally ³/ h.

Fig. 3 b illustrates the function of separation rate about particle diameter and cut-off size.Here can find out, the cut-off size of isolated particle worsens when input (dotted line and the dotted lines) of beat-type.

But the advantage of the method for operation of beat-type is main, because solid can be pooled in panel surface in the clear from volume flow here, and can be slipped in the Solid Cavity of seperator, this achieves the improvement of the clarification to liquid on the whole.

When the seperator of two series connection combines mutually, separative efficiency shown in Fig. 3 a and 3b can by the combination of two seperators to the skew in disadvantageous direction, namely become combination by non-beat-type with the separating mechanism of beat-type feed and eliminate completely, and however still achieving better clarification relative to the seperator composition cascaded structure of two non-beat-types.

In the ideal case, the cycle duration of beat should be:

$T_{\mathrm{end}}=\frac{(r_a^2-r_i^2)\mathrm{\πh}}{{\stackrel{\‾}{Q}}_T\cos \mathrm{\α}}$

Wherein, in this case it is the average inlet flow of each dish.Here better control to realize processing procedure, the frequency of beat should be less.Therefore advantageously, beat has the frequency being less than 10Hz, to avoid average risk (f=1/T).

The figure of input function except trapezoidal shown in Fig. 3 a when beat is constant also can time sinusoidal, triangle, rectangle or zigzag.

According to the present invention, centrifuge, particularly seperator have such mechanism or device, and described mechanism or device make it possible to achieve the beat of the input of the volume of the liquid that need process.

This mechanism can comprise the entrance with input pipe, and described input pipe to be configured to bending in the region of distributor, wherein realizes beat by the flank in distributor.

Alternatively, or in addition, this mechanism can comprise differential driver, between the input pipe that described differential driver is arranged on centrifuge, particularly seperator and rotary drum.According to the cycle duration of the prespecified beat of the distribution of differential driver.

Alternatively or additionally, can also on entrance or in, preferably in the flowing direction outside rotary drum or before control valve is set, the bulb valve of rotation is preferably set, or realizes input by the piston pump with constant beat.

Reference numerals list

Separator drum 1

Drive shaft 2

Case 3

Input pipe 4

Distributor 5

Outlet 6

Rising passway 7

Dish assembly 8

Separator disk 9

Solid output cavity 10

Solids outlet 11

Piston slide valve 12

Dish gap 13

Separator disk 14

Particle 16

Particle 17

Product input P

Solid phase S

Rotation Z

The inclined angle alpha of dish

Gap width h

The inside radius r of dish _i

The outer radius r of dish _a

Particle is at the spacing r (t) of time point t to rotation Z

Average inlet flow Q _t

Time t

Separative efficiency φ (d)

Diameter d

Claims (26)

1. the method for the treatment of the product that can flow, the method utilizes at least one to process by the centrifuge of continuous operation work, described centrifuge has revolvable bowl (1), setting dish assembly (8) in described bowl, described method has following steps:

A) the described product that can flow of supply in bowl (1),

B) from the product that can flow, be separated solid phase and/or the separation of products that can flow become two or more liquid phase,

C) by one or more discharge line for liquid phase, one or more liquid phase is derived from bowl (1), and, when in step b) in when also isolating solid phase, solid phase is derived from bowl (1),

It is characterized in that,

D) with the product that the volume flow supply of continuously or discontinuously beat-type need process, thus the small product size stream beat-type supplied supply, and need not close at this moment for liquid phase discharge line or additionally throttling is carried out to it.

2. method according to claim 1, is characterized in that, the supply of the product that need process is carried out with constant beat frequency.

3. method according to claim 1, is characterized in that, runs process with continuous print.

4. method according to claim 2, is characterized in that, runs process with continuous print.

5. method according to claim 1, is characterized in that, monitors, controls and/or regulate beat frequency.

6. method according to claim 2, is characterized in that, monitors, controls and/or regulate beat frequency.

7. according to the method one of the claims 2 to 4 Suo Shu, it is characterized in that, beat frequency has cycle duration, one or more relevant to following parameter of described cycle duration:

A) inside radius (r of a dish (14) of assembly (8) is coiled _i),

B) outer radius (r of described dish (14) _a),

C) inlet flow (Q of the intermediate space (13) between described dish (14) and adjacent dish (15) is entered _t),

D) angle (α) is coiled, and/or

E) spacing (h) of described dish and described adjacent dish.

8. according to the method one of claim 1 to 6 Suo Shu, it is characterized in that, the cycle duration-cycle duration T=1/ frequency f of the beat of volume flow-be less than time T _end, the described time is the time that the intermediate space (13) of particle (16,17) between a dish (14) and adjacent dish (15) of dish assembly stops, wherein

$T_{\mathrm{end}}=\frac{(r_a^2-r_i^2)\mathrm{\πh}}{Q_T\cos \mathrm{\α}}$

Wherein r _athe outer radius of described dish (14), r _ibe the inside radius of described dish (14), h is the spacing between described dish (14) and adjacent dish (15), Q _tbe the average inlet flow of each dish (14), and α is dish angle.

9. according to the method one of claim 1 to 6 Suo Shu, it is characterized in that, the cycle duration of the beat of volume flow is T _endten times, T _endit is the time that the intermediate space (13) of particle (16,17) between a dish (14) and adjacent dish (15) of dish assembly stops, wherein

$T_{\mathrm{end}}=\frac{(r_a^2-r_i^2)\mathrm{\πh}}{Q_T\cos \mathrm{\α}}$

Wherein r _athe outer radius of described dish (14), r _ibe the inside radius of described dish (14), h is the spacing between described dish (14) and adjacent dish (15), Q _tbe the average inlet flow of each dish (14), and α is dish angle.

10. according to the method one of claim 1 to 6 Suo Shu, it is characterized in that, before step a) middle input, in the first seperator, carry out the presettling of the liquid that need clarify with the input of non-beat-type.

11. methods according to claim 10, is characterized in that, and then step c) after, in the second seperator, the rear clarification of liquid is carried out with the input of non-beat-type.

12. according to the method one of claim 1 to 6 Suo Shu, it is characterized in that, the time period (T1) determining length supplies small product size (V1), the supply of the product that need process is carried out like this by the operation of beat-type, makes the supply small product size (V1) of carrying out relative to the operation by non-beat-type for each time period (T1) constant or keep constant.

13. according to the method one of claim 1 to 6 Suo Shu, it is characterized in that, the supply beat-type ground of the product that need process carries out like this, make and time correlation realize entering inlet flow that of coiling assembly coils the intermediate space (13) between (14) and adjacent dish (15) around the rising of a mean value and reduction.

14. according to the method one of claim 1 to 6 Suo Shu, it is characterized in that, the supply of the product that need process is carried out like this, and the inlet flow entering the intermediate space (13) between a dish (14) and adjacent dish (15) coiling assembly run by beat-type can not be interrupted completely.

15., according to the method one of claim 1 to 6 Suo Shu, is characterized in that, enter the inlet flow beat-type ground change per minute of the intermediate space (13) between a dish (14) of dish assembly and adjacent dish (15) repeatedly.

16. methods according to claim 15, is characterized in that, the kind change per second of inlet flow beat-type ground repeatedly.

17., according to the method one of claim 1 to 6 Suo Shu, is characterized in that, enter the inlet flow sinusoid ground change of the intermediate space (13) between a dish (14) of dish assembly and adjacent dish (15).

18., according to the method one of claim 1 to 6 Suo Shu, is characterized in that, described centrifuge is the seperator with vertical rotation.

19. 1 kinds for performing the centrifuge according to the method one of the claims Suo Shu, there is revolvable bowl, setting dish assembly in described bowl, described bowl also has at least one for supplying the input port of the product that need process and at least one is for deriving the outlet of at least one liquid phase and at least one is for deriving the outlet of at least one other phase, it is characterized in that there is the device for making the raw continuous or discrete beat of small product size miscarriage inputted in bowl.

20. centrifuges according to claim 19, is characterized in that, described device is included in the input pipe of ends bent.

21. centrifuges according to claim 19 or 20, it is characterized in that, described device has differential driver, and described differential driver is arranged between input pipe and rotary drum inner chamber or is arranged in input pipe.

22. centrifuges according to claim 19 or 20, is characterized in that, described device comprise rotation, the bulb valve be installed to before rotary drum in input port.

23. centrifuges according to claim 19 or 20, it is characterized in that, described device comprises piston pump.

24. centrifuges according to claim 19 or 20, it is characterized in that, described centrifuge is seperator.

25. centrifuges according to claim 24, is characterized in that, described bowl is the separator drum with vertical-rotation-axis.

26. centrifuges according to claim 19 or 20, is characterized in that, described at least one other be liquid phase or solid phase mutually.